WO2012175414A1 - Method for polymerizing vinylidene fluoride - Google Patents
Method for polymerizing vinylidene fluoride Download PDFInfo
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- WO2012175414A1 WO2012175414A1 PCT/EP2012/061409 EP2012061409W WO2012175414A1 WO 2012175414 A1 WO2012175414 A1 WO 2012175414A1 EP 2012061409 W EP2012061409 W EP 2012061409W WO 2012175414 A1 WO2012175414 A1 WO 2012175414A1
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08K—Use of inorganic or non-macromolecular organic substances as compounding ingredients
- C08K5/00—Use of organic ingredients
- C08K5/36—Sulfur-, selenium-, or tellurium-containing compounds
- C08K5/41—Compounds containing sulfur bound to oxygen
- C08K5/42—Sulfonic acids; Derivatives thereof
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F14/00—Homopolymers and copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by a halogen
- C08F14/18—Monomers containing fluorine
- C08F14/22—Vinylidene fluoride
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F214/00—Copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by a halogen
- C08F214/18—Monomers containing fluorine
- C08F214/22—Vinylidene fluoride
Definitions
- the invention pertains to a method for polymerizing vinylidene fluoride (VDF) for obtaining VDF polymers having increased thermal stability.
- VDF vinylidene fluoride
- Vinyiidene fluoride polymers thanks to their partially fluorinated backbone, have been long known and have been used in a variety of applications because of several desirable properties such as mechanical properties, chemical resistance, thermal resistance, etc.
- a frequently used method for producing VDF polymers involves aqueous emulsion polymerization of VDF with optionally one or more fluorinated monomers generally involving the use of fluorinated surfactants.
- fluorinated surfactants include perfluoroalkyl carboxylic acids and salts thereof.
- thermoplastic VDF polymers wherein certain partially fluorinated surfactants of general formula R f -C 2 H 4 -SO 3 M, wherein R f is a perfluorinated radical having 4 to 10 carbon atoms and M is an alkali metal such as lithium, sodium or potassium or an ammonium radical, are used, is known from US 4025709 UGINE KUHLMANN 19770524 .
- said surfactant should be used in amounts of between 0.2 to 0.5 % based on weight of water (2 to 5 g/l). Nevertheless, VDF polymers obtained from such polymerization process undergo substantial yellowing/darkening phenomena, in particular when exposed to temperature of 260°C or more, as an evidence of thermal degradation issues.
- US 6774164 DUPONT DOW ELASTOMERS L.L.C 20040810 discloses an emulsion polymerization process for the production of fluoroelastomers in the presence of a surfactant of formula F-(CF 2 CF 2 ) n -CH 2 CH 2 -SO 3 M, with n from 2 to 9, and M being a cation of valence of 1, said process being initiated by water-soluble peroxides including ammonium, sodium or potassium salts of hydrogen persulfate..
- thermoplastic VDF polymers which possess different colloidal behaviour and completely different properties.
- inorganic initiators have been used which, while known for positively affecting colloidal stability of lattices because of the formation of ionic end groups on growing chains, nevertheless lead to products having, because of these very same end-groups, moderated thermal stability, and which are prone to undergo to discoloration phenomena.
- thermoplastic VDF polymers by emulsion polymerization initiated by certain organic oxidizing agents, in the presence of a well-defined and limited amount of a particular surfactant as below detailed.
- VDF vinylidene fluoride
- polymer (F) thermoplastic polymer
- said process comprising polymerizing VDF in an aqueous phase comprising from 0.5 to 1.5 g/l of at least one surfactant of formula F-(CF 2 CF 2 ) 3 -CH 2 CH 2 -SO 3 X a , wherein X a is H, a alkali metal or a NR H 4 group, with R H being H or a C 1 -C 6 hydrocarbon group [surfactant (T)] and an organic oxidizing agent [agent (O)] as polymerization initiator.
- surfactant T
- O organic oxidizing agent
- the Applicant has surprisingly found that in above mentioned process, despite the use of such a limited amount of said surfactant (T), even in the absence of inorganic initiators, high monomer conversion, efficient nucleation and colloidal stabilization of the dispersion of the polymer (F) are achieved with substantially no polymer build-up or fouling in the reactor, and substantially no coagulation losses.
- thermoplastic is used herein to denote a semi-crystalline VDF polymer which can advantageously processed in the melt and which possesses typically a heat of fusion of more than 5 J/g, preferably more than 7 J/g, even more preferably 10 J/g, when measured according to ASTM D 3418.
- the vinylidene fluoride thermoplastic polymer is preferably a polymer comprising : (a’) at least 60 % by moles, preferably at least 75 % by moles, more preferably 85 % by moles of vinylidene fluoride (VDF); (b’) optionally from 0.1 to 15%, preferably from 0.1 to 12%, more preferably from 0.1 to 10% by moles of a fluorinated monomer different from VDF; said fluorinated monomer being preferably selected in the group consisting of vinylfluoride (VF 1 ), chlorotrifluoroethylene (CTFE), hexafluoropropene (HFP), tetrafluoroethylene (TFE), perfluoromethylvinylether (MVE), trifluoroethylene (TrFE) and mixtures therefrom; and (c’) optionally from 0.1 to 5 %, by moles, preferably 0.1 to 3 % by moles, more preferably 0.1 to 1% by mo
- the vinylidene fluoride polymer is more preferably a polymer consisting of : (a’) at least 60 % by moles, preferably at least 75 % by moles, more preferably 85 % by moles of vinylidene fluoride (VDF); (b’) optionally from 0.1 to 15%, preferably from 0.1 to 12%, more preferably from 0.1 to 10% by moles of a fluorinated monomer different from VDF; said fluorinate monomer being preferably selected in the group consisting of vinylfluoride (VF 1 ), chlorotrifluoroethylene (CTFE), hexafluoropropene (HFP), tetrafluoroethylene (TFE), perfluoromethylvinylether (MVE), trifluoroethylene (TrFE) and mixtures therefrom.
- VDF vinylidene fluoride
- b’ optionally from 0.1 to 15%, preferably from 0.1 to 12%, more preferably from 0.1 to 10% by moles of a fluor
- VDF polymers of the present invention mention can be notably made of homopolymer of VDF, VDF/TFE copolymer, VDF/TFE/HFP copolymer, VDF/TFE/CTFE copolymer, VDF/TFE/TrFE copolymer, VDF/CTFE copolymer, VDF/HFP copolymer, VDF/TFE/HFP/CTFE copolymer and the like.
- the process of the invention is particularly suitable for manufacturing VDF homopolymers.
- the melt viscosity of the polymer (F), measured at 232 ⁇ C and 100 sec -1 of shear rate according to ASTM D3835, is advantageously of at least 3 kpoise, preferably at least 5 kpoise.
- the melt viscosity of the polymer (F), measured at 232 ⁇ C and 100 sec -1 of shear rate, is advantageously of at most 60 kpois, preferably at most 40 kpoise, more preferably at most 35 kpoise.
- the melt viscosity of VDF polymer is measured in accordance with ASTM test No. D3835, run at 232°C, under a shear rate of 100 sec -1 .
- the VDF polymer has a melting point of advantageously at least 120°C, preferably at least 125°C, more preferably at least 130°C.
- the VDF polymer has a melting point advantageously of at most 190°C, preferably at most 185°C, more preferably at most 170°C.
- the melting point (T m2 ) can be determined by DSC, at a heating rate of 10°C/min, according to ASTM D 3418.
- the surfactant (T) it is essential for the surfactant (T) to be present in the aqueous phase at a concentration of 0.3 to 1.5 g/l.
- the aqueous medium comprises at least 0.3, preferably at least 0.5, more preferably at least 0.7 g/l of surfactant (T); said aqueous medium additionally comprises at most 1.5, preferably at most 1.4 g/l more preferably at most 1.3 g/l of surfactant (T).
- the polymerization process of the invention may be carried out in the presence of an additional surfactant different from surfactant (T) and used in combination thereto.
- VDF is polymerized in an aqueous phase further comprising an additional surfactant different from surfactant (T).
- said aqueous phase may comprise at least one surfactant of formula: F-(CF 2 CF 2 ) n -CH 2 CH 2 -SO 3 X’ a , with n being equal to 2 or in the range 4-7, and X’ a is H, a alkali metal or a NR H’ 4 group, with R H’ being H or a C 1 -C 6 hydrocarbon group [surfactant (Q)].
- the weight percent of surfactant (T), over the overall weight amount of surfactant (T) and surfactant (Q) used in the polymerization process of the present invention will be generally of at least 90 %wt, preferably of at least 95 % wt, more preferably of at least 99 % wt.
- the aqueous phase further comprises at least one functional (per)fluoropolyether (functional PFPE) comprising at least one (per)fluoropolyoxyalkylene chain [chain (R’ F )] and at least one functional group, said functional PFPE having a number average molecular weight of at least 1000 and a solubility in water of less than 1 % by weight at 25°C.
- functional PFPE functional fluoropolyether
- said addition of said high molecular weight functional perfluoropolyether can be beneficial for enabling efficient nucleation and tuning of the average particle size of the polymer (F).
- said functional PFPE is present in the aqueous phase in an amount of advantageously 0.001 to 0.3 g/l, preferably of 0.001 to 0.15 g/l, preferably of 0.001 to 0.1 g/l.
- the functional PFPE more preferably complies with formula (I) here below: T 1 -(CFW 1 ) p1 -O-R F -(CFW 2 ) p2 -T 2 (I) wherein: - R F is a (per)fluoropolyoxyalkylene chain [chain (R’ F )], as defined above, such that the number average molecular weight of the functional PFPE is at least 1000, preferably at least 1300, more preferably at least 1500; - T 1 and T 2 , equal to or different from each other, are selected from: i) functional end-groups selected from carboxylic acid, phosphonic acid and sulphonic acid groups, in their acid or salt form, and ii) non-functional end-groups selected from a fluorine atom, a chlorine atom and a C 1 -C 3 (per)fluoroalkyl group comprising, optionally, one or more chlorine atoms, with the proviso that at least one of T 1 and
- the aqueous phase of this embodiment preferably comprises at least one functional PFPE complying with formula (I) as described above wherein both T 1 and T 2 are functional end-groups as defined above (bifunctional PFPE).
- Non-limitative examples of suitable bifunctional PFPEs include, notably, those complying with formula (II) here below: X p OOC-CFW 1 -O-R F -CFW 2 -COOX p (II) wherein: - R F is a (per)fluoropolyoxyalkylene chain [chain (R’ F )] as defined above such that the number average molecular weight of the bifunctional PFPE is at least 1000, preferably at least 1300, more preferably at least 1500; - W 1 and W 2 , equal to or different from each other, have the same meaning as defined above; - X p , equal to or different from each other, is a hydrogen atom, a monovalent metal, preferably an alkaline metal, or an ammonium group of formula -N(R’ n ) 4 , wherein R’ n , equal or different at each occurrence, is a hydrogen atom or a C 1 -C 6 hydrocarbon group, preferably an al
- More preferred aqueous phases comprise at least one bifunctional PFPE complying with formula (III) here below: X p OOC-CF 2 -O-(CF 2 ) n’ (CF 2 CF 2 O) m’ -CF 2 -COOX p (III) wherein n’ and m’ are independently integers > 0 such that the number average molecular weight of the bifunctional PFPE is at least 1000, preferably at least 1300, more preferably at least 1500, the recurring units being generally statistically distributed along the perfluoropolyoxyalkylene chain, and X p has the meaning as above defined.
- the polymerization process of the invention is started by a polymerization initiator which is an organic oxidizing agent [agent (O)].
- agent (O) is generally selected from the group consisting of: - diacylperoxides such as diacetylperoxide, disuccinyl peroxide, dipropionylperoxide, dibutyrylperoxide, dibenzoylperoxide, benzoylacetylperoxide, diglutaric acid peroxide and dilaurylperoxide; - dialkylperoxides, including notably ditertbutylperoxide (DTBP), dicumyl peroxide, tert-butylcumyl peroxide, 1,3-1,4-bis(tert-butylperoxyisopropyl)benzene, 2,5 dimethyl 2,5 di(tert-butylperoxyl) hexyne, 2,5-dimethyl-2,5-di(tert-butylperoxyl) hexan
- per-acids include peracetic acid
- esters of the peracids can be used as well and examples thereof include alkylperoxyacetates, alkylperoxybenzoates, alkylperoxypivalates, like notably tert-butylperoxyacetate and tert-butylperoxypivalate
- - peroxydicarbonates including notably diisopropylperoxydicarbonate, di-n-propylperoxydicarbonate.
- Dialkylperoxides and hydroalkylperoxides, as above detailed, are generally preferred. Among those compounds, DTBP is particularly advantageous.
- the amount of initiator typically ranges between 0.01% and 1% by weight, preferably between 0.01 and 0.5% by weight with respect to the weight of the polymer (F) to be produced.
- the polymerization process may be carried out in the presence of other materials such as, notably, chain-transfer agents.
- chain transfer agents suitable for the purpose of the process of the invention include, notably, compounds of formula R f (I) x (Br) y , wherein R f is a C 1 -C 8 (per)fluoro(chloro)alkyl group, x and y are independently integers between 0 and 2, the (x+y) sum being comprised between 1 and 2, such as, e.g., 1,4-diiodoperfluorobutane.
- Chain-transfer agents which may be used include, notably, C 1 -C 5 alkanes such as, e.g., ethane, propane and n-pentane, halogenated hydrocarbons such as, e.g., CCl 4 , CHCl 3 , CH 2 Cl 2 , hydrofluorocarbon compounds such as, e.g., CH 2 F-CF 3 (R134a), ethers such as, e.g., dimethyl ether and methyl tert -butyl ether and esters such as, e.g., ethyl acetate and malonic esters.
- C 1 -C 5 alkanes such as, e.g., ethane, propane and n-pentane
- halogenated hydrocarbons such as, e.g., CCl 4 , CHCl 3 , CH 2 Cl 2
- hydrofluorocarbon compounds such as, e.g., CH 2 F-CF
- the process of the invention generally comprises the following steps: a) feeding an aqueous solution of the surfactant (T) into the polymerization reactor, possibly in combination with deionized water, so as to achieve the required concentration of surfactant (T) in the aqueous phase; b) optionally adding into the aqueous medium chain transfer agent(s), stabilizer(s) and/or other polymerization additive(s); d) adding vinylidene fluoride (VDF), possibly in combination with other copolymerizable monomers, if required; d) adding the polymerization initiator and, optionally, during the polymerization, further adding additional amounts of VDF monomer and/or comonomers, initiators, transfer agents; f) recovering from the reactor the polymer (F) dispersion.
- VDF vinylidene fluoride
- Polymerization is generally carried out at a pressure of at least 350 psi, preferably of at least 400 psi, more preferably of at least 500 psi.
- Polymerization can be carried out at a temperature of at least 50°C, preferably of at least 60°C, more preferably of at least 80°C.
- Upper temperature is not particularly limited, provided that an aqueous phase is maintained in polymerization conditions. Generally temperature will not exceed 130°C, preferably 125°C.
- Comparative Example 1 A 7.5 litre stainless steel horizontal reactor equipped with a stirrer was charged with 5 375 g of demineralized water and an aqueous solution of a surfactant of formula F-(CF 2 CF 2 ) 3 -CH 2 CH 2 -SO 3 H, in such amount that its concentration in the aqueous phase of the reactor was 2.4 g/l. 4 g of paraffinic wax having a melting point between 50° and 60°C were then added. The reactor was sealed and heated to 100°C under stirring, degassing for about 2 minutes. The-reactor was heated up to 122.5°C; then vinylidene fluoride was fed into the reactor to reach an inner pressure to 45 bar.
- a surfactant of formula F-(CF 2 CF 2 ) 3 -CH 2 CH 2 -SO 3 H
- the reactor was washed to remove the possible coagulum formed during to polymerization. A loss of 2.4% due to the coagulum was evaluated (defined as the percentage of coagulated particles with respect to the initial weight of 2 298 g of vinylidene fluoride).
- the filtered latex is analyzed by laser light scattering technique and was found to have an average size of the particle diameter of 0.239 ⁇ m.
- the latex was then coagulated by mechanical stirring; the coagulated polymer was washed several times with demineralized water until the washing water conductivity decreases of less than 2 ⁇ ohm/cm.
- the wet polymer was dried in a convection stove at 60°C, until the moisture content was lower than 0.15% by weight.
- a very dark specimen was obtained when coagulated product was melted.
- Yellow Index measured after thermal aging of the dried powder at 270°C for 1 hour was found to be 83.3.
- Example 2 Same procedure as in example 1 was followed but using an amount of surfactant of formula F-(CF 2 CF 2 ) 3 -CH 2 CH 2 -SO 3 H so as to yield a concentration of 1.2 g/l in the aqueous phase.
- the latex After 208 minutes of polymerization, the latex was found to contain 29.7% by weight of polymer having an average size of the particle diameter of 0.297 ⁇ m, with a 4.3% wt loss due to the coagulum.
- the latex After 199 minutes of polymerization, the latex was found to contain 29.7% by weight of polymer having an average size of the particle diameter of 0.282 ⁇ m, with a 3.9 % wt loss due to the coagulum.
- Yellow Index measured after thermal aging of the dried powder at 270°C for 1 hour was found to be 40.0.
- the latex After 186 minutes of polymerization, the latex was found to contain 29.8% by weight of polymer having an average size of the particle diameter of 0.306 ⁇ m, with a 4.6 % wt loss due to the coagulum.
- Yellow Index measured after thermal aging of the dried powder at 270°C for 1 hour was found to be 41.6.
- the latex was found to contain 27.2% by weight of polymer having an average size of the particle diameter of 0.291 ⁇ m, with a 4.8 % wt loss due to the coagulum.
- Yellow Index measured after thermal aging of the dried powder at 270°C for 1 hour was found to be 57.0.
- Example 5 Similar procedure as in Example 5 was followed, but using a 21 liter stainless steel horizontal reactor equipped with a stirrer, 14.1 L of demineralized water, an aqueous solution of a surfactant of formula F-(CF 2 CF 2 ) 3 -CH 2 CH 2 -SO 3 H, in such amount that its concentration in the aqueous phase of the reactor is 1.0 g/l, and adding same bifunctional fluorinated surfactant of Example 5 in such amount that its concentration in the aqueous phase of the reactor was 50 mg/l.
- Polymerization temperature was set to 85°C and set point pressure of 30 bar was initially achieved by feeding a mixture of VDF 72.5% by moles and HFP 27.5% by moles.
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Abstract
Description
Nevertheless, VDF polymers obtained from such polymerization process undergo substantial yellowing/darkening phenomena, in particular when exposed to temperature of 260°C or more, as an evidence of thermal degradation issues.
(a’) at least 60 % by moles, preferably at least 75 % by moles, more preferably 85 % by moles of vinylidene fluoride (VDF);
(b’) optionally from 0.1 to 15%, preferably from 0.1 to 12%, more preferably from 0.1 to 10% by moles of a fluorinated monomer different from VDF; said fluorinated monomer being preferably selected in the group consisting of vinylfluoride (VF1), chlorotrifluoroethylene (CTFE), hexafluoropropene (HFP), tetrafluoroethylene (TFE), perfluoromethylvinylether (MVE), trifluoroethylene (TrFE) and mixtures therefrom; and
(c’) optionally from 0.1 to 5 %, by moles, preferably 0.1 to 3 % by moles, more preferably 0.1 to 1% by moles, based on the total amount of monomers (a’) and (b’), of one or more hydrogenated comonomer(s).
(a’) at least 60 % by moles, preferably at least 75 % by moles, more preferably 85 % by moles of vinylidene fluoride (VDF);
(b’) optionally from 0.1 to 15%, preferably from 0.1 to 12%, more preferably from 0.1 to 10% by moles of a fluorinated monomer different from VDF; said fluorinate monomer being preferably selected in the group consisting of vinylfluoride (VF1), chlorotrifluoroethylene (CTFE), hexafluoropropene (HFP), tetrafluoroethylene (TFE), perfluoromethylvinylether (MVE), trifluoroethylene (TrFE) and mixtures therefrom.
F-(CF2CF2)n-CH2CH2-SO3X’a, with n being equal to 2 or in the range 4-7, and X’a is H, a alkali metal or a NRH’ 4 group, with RH’ being H or a C1-C6 hydrocarbon group [surfactant (Q)].
T1-(CFW1)p1-O-RF-(CFW2)p2-T2 (I)
wherein:
- RF is a (per)fluoropolyoxyalkylene chain [chain (R’F)], as defined above, such that the number average molecular weight of the functional PFPE is at least 1000, preferably at least 1300, more preferably at least 1500;
- T1 and T2, equal to or different from each other, are selected from:
i) functional end-groups selected from carboxylic acid, phosphonic acid and sulphonic acid groups, in their acid or salt form, and
ii) non-functional end-groups selected from a fluorine atom, a chlorine atom and a C1-C3 (per)fluoroalkyl group comprising, optionally, one or more chlorine atoms,
with the proviso that at least one of T1 and T2 is a functional end-group as defined above;
- W1 and W2, equal to or different from each other, independently represent a fluorine atom or a -CF3 group;
- p1 and p2, equal to or different from each other, are independently integers comprised between 1 and 3, preferably being equal to 1 when W1 and/or W2 are -CF3 groups.
XpOOC-CFW1-O-RF-CFW2-COOXp (II)
wherein:
- RF is a (per)fluoropolyoxyalkylene chain [chain (R’F)] as defined above such that the number average molecular weight of the bifunctional PFPE is at least 1000, preferably at least 1300, more preferably at least 1500;
- W1 and W2, equal to or different from each other, have the same meaning as defined above;
- Xp , equal to or different from each other, is a hydrogen atom, a monovalent metal, preferably an alkaline metal, or an ammonium group of formula -N(R’n)4, wherein R’n, equal or different at each occurrence, is a hydrogen atom or a C1-C6 hydrocarbon group, preferably an alkyl group.
XpOOC-CF2-O-(CF2)n’(CF2CF2O)m’-CF2-COOXp (III)
wherein n’ and m’ are independently integers > 0 such that the number average molecular weight of the bifunctional PFPE is at least 1000, preferably at least 1300, more preferably at least 1500, the recurring units being generally statistically distributed along the perfluoropolyoxyalkylene chain, and Xp has the meaning as above defined.
- diacylperoxides such as diacetylperoxide, disuccinyl peroxide, dipropionylperoxide, dibutyrylperoxide, dibenzoylperoxide, benzoylacetylperoxide, diglutaric acid peroxide and dilaurylperoxide;
- dialkylperoxides, including notably ditertbutylperoxide (DTBP), dicumyl peroxide, tert-butylcumyl peroxide, 1,3-1,4-bis(tert-butylperoxyisopropyl)benzene, 2,5 dimethyl 2,5 di(tert-butylperoxyl) hexyne, 2,5-dimethyl-2,5-di(tert-butylperoxyl) hexane;
- hydroalkylperoxides, including notably t-butyl hydroperoxide (TBHP), cumene hydroperoxide, tertiaryamylhydroperoxide;
- percarboxylic acids esters and salts thereof such as e.g. ammonium, sodium or potassium salt; examples of per-acids include peracetic acid; esters of the peracids can be used as well and examples thereof include alkylperoxyacetates, alkylperoxybenzoates, alkylperoxypivalates, like notably tert-butylperoxyacetate and tert-butylperoxypivalate;
- peroxydicarbonates, including notably diisopropylperoxydicarbonate, di-n-propylperoxydicarbonate.
a) feeding an aqueous solution of the surfactant (T) into the polymerization reactor, possibly in combination with deionized water, so as to achieve the required concentration of surfactant (T) in the aqueous phase;
b) optionally adding into the aqueous medium chain transfer agent(s), stabilizer(s) and/or other polymerization additive(s);
d) adding vinylidene fluoride (VDF), possibly in combination with other copolymerizable monomers, if required;
d) adding the polymerization initiator and, optionally, during the polymerization, further adding additional amounts of VDF monomer and/or comonomers, initiators, transfer agents;
f) recovering from the reactor the polymer (F) dispersion.
A 7.5 litre stainless steel horizontal reactor equipped with a stirrer was charged with 5 375 g of demineralized water and an aqueous solution of a surfactant of formula F-(CF2CF2)3-CH2CH2-SO3H, in such amount that its concentration in the aqueous phase of the reactor was 2.4 g/l.
4 g of paraffinic wax having a melting point between 50° and 60°C were then added. The reactor was sealed and heated to 100°C under stirring, degassing for about 2 minutes. The-reactor was heated up to 122.5°C; then vinylidene fluoride was fed into the reactor to reach an inner pressure to 45 bar. The addition of 24.4 ml of di-tertbutyl peroxide (DTBP) initiator was used to start the polymerization. The vinylidene fluoride was continuously added to maintain the reactor pressure at set-point value of 45 bar. About 239 minutes, time necessary for the time necessary for the introduction of a total amount of 2 298 g of monomer, VDF feed was stopped. To optimize the yield, the polymerization was allowed to continue until the reactor pressure decreases to about 11bar. At this point the reactor was cooled, the unreacted vinylidene fluoride was vented, then the latex was discharged from the reactor and filtered on 80 mesh to remove possible coagula. The latex was found to contain 29.4% by weight of polymer. The reactor was washed to remove the possible coagulum formed during to polymerization. A loss of 2.4% due to the coagulum was evaluated (defined as the percentage of coagulated particles with respect to the initial weight of 2 298 g of vinylidene fluoride). The filtered latex is analyzed by laser light scattering technique and was found to have an average size of the particle diameter of 0.239 μm. The latex was then coagulated by mechanical stirring; the coagulated polymer was washed several times with demineralized water until the washing water conductivity decreases of less than 2 μohm/cm. The wet polymer was dried in a convection stove at 60°C, until the moisture content was lower than 0.15% by weight. The polymer melt viscosity, measured at 232°C and shear rate 100 s−1 with the Kayeness Galaxy capillary rheometer (L/D=15/1) was found to be of 18.9 kP.
A very dark specimen was obtained when coagulated product was melted. Yellow Index measured after thermal aging of the dried powder at 270°C for 1 hour was found to be 83.3.
Same procedure as in example 1 was followed but using an amount of surfactant of formula F-(CF2CF2)3-CH2CH2-SO3H so as to yield a concentration of 1.2 g/l in the aqueous phase.
After 208 minutes of polymerization, the latex was found to contain 29.7% by weight of polymer having an average size of the particle diameter of 0.297 μm, with a 4.3% wt loss due to the coagulum.
The polymer melt viscosity, measured as above, was of 23.9 kP.
Yellow Index measured after thermal aging of the dried powder at 270°C for 1 hour was found to be 66.0.
After 187 minutes of polymerization, the latex was found to contain 29.9% by weight of polymer having an average size of the particle diameter of 0.274 μm, with a 3.0% wt loss due to the coagulum.
The polymer melt viscosity, measured as above, was of 32.7 kP.
Yellow Index measured after thermal aging of the dried powder at 270°C for 1 hour was found to be 49.5.
After 170 minutes of polymerization, the latex was found to contain 29.7% by weight of polymer having an average size of the particle diameter of 0.192 μm, with a 2.9 % wt loss due to the coagulum.
The polymer melt viscosity, measured as above, was of 31.7 kP.
Yellow Index measured after thermal aging of the dried powder at 270°C for 1 hour was found to be 48.3.
After 203 minutes of polymerization, the latex was found to contain 29.2% by weight of polymer having an average size of the particle diameter of 0.302 μm, with a 2.5 % wt loss due to the coagulum.
The polymer melt viscosity, measured as above, was of 33.9 kP.
Yellow Index measured after thermal aging of the dried powder at 270°C for 1 hour was found to be 38.2.
The polymer melt viscosity, measured as above, was of 21.6 kP.
Yellow Index measured after thermal aging of the dried powder at 270°C for 1 hour was found to be 72.
Claims (10)
- A process for manufacturing a dispersion of a vinylidene fluoride (VDF) thermoplastic polymer [polymer (F)], said process comprising polymerizing VDF in an aqueous phase comprising from 0.5 to 1.5 g/l of at least one surfactant of formula F-(CF2CF2)3-CH2CH2-SO3Xa, wherein Xa is H, a alkali metal or a NRH 4 group, with RH being H or a C1-C6 hydrocarbon group [surfactant (T)] and an organic oxidizing agent [agent (O)] as polymerization initiator.
- The process of claim 1, wherein said polymer (F) is a polymer comprising :(a’) at least 60 % by moles, preferably at least 75 % by moles, more preferably 85 % by moles of vinylidene fluoride (VDF);(b’) optionally from 0.1 to 15%, preferably from 0.1 to 12%, more preferably from 0.1 to 10% by moles of a fluorinated monomer different from VDF; said fluorinated monomer being preferably selected in the group consisting of vinylfluoride (VF1), chlorotrifluoroethylene (CTFE), hexafluoropropene (HFP), tetrafluoroethylene (TFE), perfluoromethylvinylether (MVE), trifluoroethylene (TrFE) and mixtures therefrom; and(c’) optionally from 0.1 to 5 %, by moles, preferably 0.1 to 3 % by moles, more preferably 0.1 to 1% by moles, based on the total amount of monomers (a’) and (b’), of one or more hydrogenated comonomer(s).
- The process of anyone of claims 1 to 2, wherein the aqueous phase comprises an amount of 0.8 to 1.2 g/l of surfactant (T).
- The process of anyone of claims 1 to 3, wherein the aqueous phase further comprises an additional surfactant different from surfactant (T), said additional surfactant complying with formula:F-(CF2CF2)n-CH2CH2-SO3X’a, with n being equal to 2 or in the range 4-7, and X’a is H, a alkali metal or a NRH’ 4 group, with RH’ being H or a C1-C6 hydrocarbon group [surfactant (Q)].
- The process of claim 4, wherein the weight percent of surfactant (T), over the overall weight amount of surfactant (T) and surfactant (Q), is of at least 90 %wt, preferably of at least 95 % wt, more preferably of at least 99 % wt.
- The process according to anyone of claims 1 to 5, wherein the aqueous phase further comprises at least one functional (per)fluoropolyether (functional PFPE) comprising at least one (per)fluoropolyoxyalkylene chain [chain (R’F)] and at least one functional group, said functional PFPE having a number average molecular weight of at least 1000 and a solubility in water of less than 1 % by weight at 25°C.
- The process of claim 6, wherein aqueous phases comprise at least one bifunctional PFPE complying with formula (III) here below:XpOOC-CF2-O-(CF2)n’(CF2CF2O)m’-CF2-COOXp (III)wherein n’ and m’ are independently integers > 0 such that the number average molecular weight of the bifunctional PFPE is at least 1000, preferably at least 1300, more preferably at least 1500, the recurring units being generally statistically distributed along the perfluoropolyoxyalkylene chain, and each of Xp, equal to or different from each other, is a hydrogen atom, a monovalent metal, preferably an alkaline metal, or an ammonium group of formula -N(R’n)4, wherein R’n, equal or different at each occurrence, is a hydrogen atom or a C1-C6 hydrocarbon group, preferably an alkyl group
- The process of anyone of claims 1 to 7, wherein the agent (O) is selected from the group consisting of:- diacylperoxides;- dialkylperoxides;- hydroalkylperoxides;- percarboxylic acids esters and salts thereof;- peroxydicarbonates.
- The process of claim 8, wherein the agent (O) is selected from the group consisting of- diacylperoxides selected from the group consisting of diacetylperoxide, disuccinyl peroxide, dipropionylperoxide, dibutyrylperoxide, dibenzoylperoxide, benzoylacetylperoxide, diglutaric acid peroxide and dilaurylperoxide;- dialkylperoxides selected from the group consisting of ditertbutylperoxide (DTBP), dicumyl peroxide, tert-butylcumyl peroxide, 1,3-1,4-bis(tert-butylperoxyisopropyl)benzene, 2,5 dimethyl 2,5 di(tert-butylperoxyl) hexyne, and 2,5-dimethyl-2,5-di(tert-butylperoxyl) hexane;- hydroalkylperoxides, selected from the group consisting of t-butyl hydroperoxide (TBHP), cumene hydroperoxide, and tertiaryamylhydroperoxide;- percarboxylic acids esters and salts thereof selected from the group consisting of peracetic acid salts and alkylperoxyacetates, alkylperoxybenzoates, alkylperoxypivalates esters;- peroxydicarbonates selected from the group consisting of diisopropylperoxydicarbonate, and di-n-propylperoxydicarbonate.
- The process of claim 8 or 9, wherein the agent (O) is selected from dialkylperoxides and hydroalkylperoxides.
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN201280040786.9A CN103748120A (en) | 2011-06-21 | 2012-06-15 | Method for polymerizing vinylidene fluoride |
EP12730438.4A EP2723784B1 (en) | 2011-06-21 | 2012-06-15 | Method for polymerizing vinylidene fluoride |
US14/125,940 US9534106B2 (en) | 2011-06-21 | 2012-06-15 | Method for polymerizng vinylidene fluoride |
JP2014516283A JP6005737B2 (en) | 2011-06-21 | 2012-06-15 | Method for polymerizing vinylidene fluoride |
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Application Number | Priority Date | Filing Date | Title |
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US201161499341P | 2011-06-21 | 2011-06-21 | |
US61/499,341 | 2011-06-21 | ||
EP11176240.7 | 2011-08-02 | ||
EP11176240 | 2011-08-02 |
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WO2012175414A1 true WO2012175414A1 (en) | 2012-12-27 |
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PCT/EP2012/061409 WO2012175414A1 (en) | 2011-06-21 | 2012-06-15 | Method for polymerizing vinylidene fluoride |
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US (1) | US9534106B2 (en) |
EP (1) | EP2723784B1 (en) |
JP (1) | JP6005737B2 (en) |
CN (2) | CN103748120A (en) |
WO (1) | WO2012175414A1 (en) |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2015031569A1 (en) * | 2013-08-30 | 2015-03-05 | Arkema Inc. | Fluoropolymer blend |
US20160215120A1 (en) * | 2013-09-30 | 2016-07-28 | Arkema Inc. | Heat stabilized polyvinylidene fluoride polymer composition |
US10150820B2 (en) | 2012-12-28 | 2018-12-11 | Daikin Industries, Ltd. | Production method for polyvinylidene fluoride aqueous dispersion liquid, and polyvinylidene fluoride aqueous dispersion liquid |
WO2019076901A1 (en) * | 2017-10-17 | 2019-04-25 | Solvay Specialty Polymers Italy S.P.A. | Method for the synthesis of fluoropolymers |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US9534106B2 (en) * | 2011-06-21 | 2017-01-03 | Solvay Specialty Polymers Italy S.P.A. | Method for polymerizng vinylidene fluoride |
CN104448094A (en) * | 2014-12-06 | 2015-03-25 | 常熟丽源膜科技有限公司 | Production process of polyvinylidene fluoride with thermal stability |
FR3044672B1 (en) * | 2015-12-02 | 2017-11-24 | Arkema France | EXTRUSION AGENT FOR POLYOLEFINS |
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- 2012-06-15 US US14/125,940 patent/US9534106B2/en not_active Expired - Fee Related
- 2012-06-15 CN CN201280040786.9A patent/CN103748120A/en active Pending
- 2012-06-15 EP EP12730438.4A patent/EP2723784B1/en not_active Not-in-force
- 2012-06-15 JP JP2014516283A patent/JP6005737B2/en not_active Expired - Fee Related
- 2012-06-15 WO PCT/EP2012/061409 patent/WO2012175414A1/en active Application Filing
- 2012-06-15 CN CN201910508434.5A patent/CN110256615A/en active Pending
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Also Published As
Publication number | Publication date |
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EP2723784A1 (en) | 2014-04-30 |
US9534106B2 (en) | 2017-01-03 |
CN110256615A (en) | 2019-09-20 |
EP2723784B1 (en) | 2017-01-11 |
JP6005737B2 (en) | 2016-10-12 |
US20140121321A1 (en) | 2014-05-01 |
CN103748120A (en) | 2014-04-23 |
JP2014517128A (en) | 2014-07-17 |
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